JP2016191074A - Ethylene polymer particle, manufacturing method thereof and molded article using the same - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide an ethylene polymer particle obtainable by a solid phase method such as solid phase drawing molding, and appropriate for providing a molded article with high strength.SOLUTION: There is provided an ethylene polymer particle having a specific shape on a particle surface, with 5 to 30 dl/g intrinsic viscosity [η], and 80% or higher crystallinity, which is high. The ethylene polymer fine particle can be obtained by polymerizing an olefin including ethylene, using an olefin polymerization catalyst including a solid titanium catalyst component containing magnesium, halogen and titanium, under a specific condition, for instance.SELECTED DRAWING: Figure 1

Description

  The present invention relates to an ethylene polymer particle having an extremely high molecular weight, a high degree of crystallinity, and a specific surface shape. Moreover, it is related with the molded article obtained by using said ethylene polymer particle.

  The so-called ultra-high molecular weight ethylene polymer, which has an extremely high molecular weight, is superior in impact resistance, wear resistance, chemical resistance, strength, etc. compared to general-purpose ethylene polymers, and has excellent characteristics as an engineering plastic. doing.

  Such an ultrahigh molecular weight ethylene polymer is a so-called Ziegler catalyst comprising a halogen-containing transition metal compound and an organometallic compound, Japanese Patent Application Laid-Open No. 3-130116 (Patent Document 1), or Japanese Patent Application Laid-Open No. 7-156173 (Patent). It is known that it can be obtained by a known catalyst such as a magnesium compound-supported catalyst described in literature 2). In recent years, from the viewpoint of production efficiency and the like, ultra high molecular weight ethylene polymers are often produced with highly active catalysts such as magnesium compound supported catalysts.

  On the other hand, ultrahigh molecular weight ethylene polymers are difficult to perform melt molding, which is a general resin molding method, because of their high molecular weight. For this reason, molding methods such as gelling ultra-high molecular weight ethylene polymers and solid-phase stretching methods in which ultra-high molecular weight ethylene polymer particles are stretched after being crimped at a temperature below the melting point have been developed. The above-mentioned patent document 2, JP-A-9-254252 (patent document 3), JP-A 63-41512 (patent document 4), JP-A 63-66207 (patent document 5), etc. ing.

JP-A-3-130116 JP 7-156173 A JP-A-9-254252 JP-A-63-41512 JP-A 63-66207

  In the specific molding method using polymer particles such as the above-mentioned solid phase stretching method, the polymer particles are pressed at a temperature below the melting point of the particles, so that the strength of the resulting molded product is relatively low. It is said that there is. In order to overcome this problem, ethylene polymer particles having high crystallinity and heat of fusion are required.

  Conventionally, it has been said that ethylene polymer particles having few surface irregularities are suitable for solid-phase stretch molding. However, the present inventors have found that polymer particles having a specific shape with many irregularities on the surface can solve the above-mentioned problems because the contact points and the contact area increase when the particles come into contact with each other. The present inventors have also found that the polymer particles are suitable for solid phase stretch molding and have completed the present invention.

That is, the present invention
(I) The intrinsic viscosity [η] is in the range of 5 dl / g to 30 dl / g,
(II) the degree of crystallinity is 80% or more,
(III) An ethylene polymer fine particle having a shape with a thickness of 0.1 μm to 3 μm and a length of 2 μm to 20 μm on the particle surface, and a method for producing the same.
Moreover, this invention provides the molded article obtained using said ethylene polymer particle. Furthermore, this invention is providing the said molded article obtained by a solid-phase stretching method.

  Since the ethylene polymer particles of the present invention have an extremely high molecular weight, a high crystallinity, and a specific surface shape, a high-strength molded product can be obtained, for example, when solid-phase stretch molding is performed.

It is a SEM photograph of the ethylene polymer particle of Example 1 of this invention.

(Ethylene polymer particles)
In the present invention, the copolymerization may be referred to as polymerization, and the copolymer may be referred to as a polymer. An ethylene polymer having an intrinsic viscosity [η] of 5 dl / g or more is sometimes referred to as an ultrahigh molecular weight ethylene polymer.

The ultrahigh molecular weight ethylene polymer particles of the present invention are characterized by satisfying the following conditions.
(I) The intrinsic viscosity [η] is in the range of 5 dl / g to 30 dl / g,
(II) the degree of crystallinity is 80% or more,
(III) The particle surface has a shape with a thickness of 0.1 μm to 3 μm and a length of 2 μm to 20 μm.

  The intrinsic viscosity is a value measured at 135 ° C. in a decalin solvent. The range of intrinsic viscosity [η] is preferably 8 dl / g to 25 dl / g, more preferably 10 dl / g to 25 dl / g, still more preferably 15 dl / g to 25 dl / g.

  The degree of crystallinity is 80% or more, preferably 80% to 90%, more preferably 80% to 88%. The crystallinity is a value measured by X-ray crystal analysis using a RINT2500 type apparatus manufactured by Rigaku Corporation.

  The ultra high molecular weight ethylene polymer particles of the present invention are suitable for solid phase stretch molding as described later. When ultra-high molecular weight ethylene polymer is molded at a temperature below the melting point as in solid phase stretch molding, the ratio between the crystalline part and the amorphous part and the entanglement between molecules are the major factors governing moldability. Conceivable.

  The ethylene polymer particles having a high crystallinity as described above are considered to contribute to the high strength of the solid-phase stretched molded product. In addition, ethylene polymer particles having a high degree of crystallinity tend to hardly undergo distortion or deformation such as volume shrinkage because the change in crystallinity is small during solid-phase stretch molding at a relatively high temperature. This is presumed to be one reason that the ethylene polymer particles of the present invention are considered to exhibit good moldability.

  The ultrahigh molecular weight ethylene polymer of the present invention is a homopolymer of ethylene, ethylene and a small amount of α-olefin such as propylene, 1-butene, 4-methyl-1-pentene, 1-pentene, 1-hexene, 1-hexene, Examples thereof include crystalline copolymers mainly composed of ethylene obtained by copolymerizing octene, 1-decene, etc., from the viewpoint of increasing the crystallinity and the stretchability in the solid-phase stretch molding described later. Is preferably an ethylene homopolymer. Even if it is a homopolymer of ethylene, an ultrahigh molecular weight ethylene polymer having a branched structure may be obtained depending on the olefin polymerization catalyst used, but the ultrahigh molecular weight ethylene polymer particles of the present invention may have such a branched structure. It is preferable that there is no.

  The ultra high molecular weight ethylene polymer particles as described above may be used in combination with various known stabilizers as necessary. Examples of such a stabilizer include heat-resistant stabilizers such as tetrakis [methylene (3,5-di-t-butyl-4-hydroxy) hydrocinnamate] methane and distearyl thiodipropionate, or bis (2 , 2 ', 6,6'-tetramethyl-4-piperidine) sebacate, 2- (2-hydroxy-t-butyl-5-methylphenyl) -5-chlorobenzotriazole, and the like. . An inorganic or organic dry color may be added as a colorant. Further, stearates such as calcium stearate known as lubricants and hydrogen chloride absorbents can also be mentioned as suitable stabilizers.

  The ultra high molecular weight ethylene polymer particles of the present invention have a thickness of 0.1 μm to 3 μm, preferably 0.2 μm to 2.5 μm, more preferably 0.2 μm to 1.5 μm, and particularly preferably 0 on the particle surface. It is characterized by having a shape of 2 μm to 1.0 μm and a length of 2 μm to 20 μm, preferably 3 μm to 18 μm. This so-called thread-like or columnar shape can be confirmed by SEM observation. The thickness and length of the filamentous shape specified in the present invention are determined by SEM observation using a JSM-6300F scanning electron microscope apparatus manufactured by JEOL.

  Since the ultrahigh molecular weight ethylene polymer particles having such a thread-like or columnar structure have many irregularities on the particle surface and a large surface area, the contact area when the ultrahigh molecular weight ethylene polymer particles are brought into contact with each other is large. It tends to be wide. When the contact area between the ethylene polymer particles is large, the particles tend to be pressed when they are formed by the solid-phase stretching method described later.

The ethylene polymer particles of the present invention preferably have an average particle size of 100 μm to 300 μm and a content of particles having a particle size of 355 μm or more of 2% by mass or less. The lower limit of the average particle diameter is preferably 110 μm, more preferably 120 μm, particularly preferably 130 μm.
On the other hand, the preferable upper limit is 280 μm, more preferably 260 μm.

  As the average particle size of the ethylene polymer particles produced when producing ethylene polymer particles by polymerization of ethylene and other olefins used as necessary increases, the heat of polymerization reaction tends to stay in the particles. There is a possibility that partial melting of particles and fusion between particles may occur. When such melting or fusion occurs, it is estimated that the entanglement of the polymer chains of the ethylene polymer particles increases. Such an increase in the entanglement of the polymer chains tends to cause a decrease in the drawing performance of the resin for solid phase drawing molding. Therefore, if the average particle size exceeds the upper limit of the particle size, the moldability during solid phase stretching may be reduced.

  Further, when the average particle diameter of the ethylene polymer particles is less than the lower limit value of the particle diameter, there may be a problem in handling due to easy charging.

In the ethylene polymer particles of the present invention, the content of particles having a particle size of 355 μm or more is preferably 1.5% by mass or less, more preferably 1.0% by mass or less.
The presence of coarse particles having a particle size exceeding 355 μm may impair the uniformity of the molded product during the production of a solid-phase stretch molded product. For example, when producing a compressed sheet, which is the first stage in the production of a stretched molded product to be described later, a portion where coarse particles are present may disturb the uniformity of the sheet. This nonuniformity is the starting point, which may cause the sheet to break in the stretch forming process from the second stage onward, leading to a decrease in the stretch ratio.

  The average particle diameter of the ethylene polymer particles of the present invention is a so-called median diameter, and a sieving method for measuring the particle size distribution of the ethylene polymer particles by stacking 6 to 8 types of sieves having different openings in multiple stages. Can be measured. If there is a sieve having an opening diameter of 355 μm in the sieve, the content of the coarse particles can be measured simultaneously.

[Olefin polymerization catalyst]
The ultrahigh molecular weight ethylene polymer particles of the present invention can use any known olefin polymerization catalyst without limitation as long as the above intrinsic viscosity and shape can be realized. Preferably, the olefin polymerization catalyst is a highly active catalyst containing a solid catalyst component and producing 500 g or more of an ethylene polymer per 1 g of the solid catalyst component. More preferably, a catalyst component that produces 1,000 g or more, more preferably 2,000 g or more of an ethylene polymer per 1 g of the solid catalyst component is used. There is not much meaning in setting the upper limit of the so-called polymerization activity, but in consideration of the risk of melting the ethylene polymer generated by the heat of polymerization reaction, less than 60,000 g-polymer / g-solid catalyst component or less. Preferably, it is 30,000 g-polymer / g-solid catalyst component or less.

  The ethylene polymer particles produced from the solid catalyst component are said to be an aggregate of ethylene polymer lumps produced at active sites in the solid catalyst component. Since the solid high activity catalyst as described above has a relatively large number of active points in the catalyst, the ethylene polymer particles produced from the solid catalyst component are aggregates of more ethylene polymer lumps. Therefore, it is thought that it is easy to take the structure where the surface area of ethylene polymer particles is wide. In addition, since such a solid catalyst has high activity, it is estimated that a part of the generated polyolefin is ejected from the pores of the solid catalyst component to form thread-like and columnar shapes.

As a preferable example of the olefin polymerization catalyst as described above,
[A] a solid titanium catalyst component containing magnesium, halogen, titanium, and
[B] An olefin polymerization catalyst containing an organometallic compound catalyst component containing a metal element selected from Group 1, Group 2 and Group 13 of the periodic table can be mentioned. Examples of these catalysts are described in detail below.

[Solid titanium catalyst component [A]]
The above-mentioned solid titanium catalyst component [A] containing titanium, magnesium and halogen is disclosed in JP-A-56-811, JP-A-57-63310, in addition to the above-mentioned Patent Documents 1 and 2. Examples of the solid titanium catalyst component described in JP-A-58-83006, JP-A-3-706, JP-A-2-255810, JP-A-4-218509, and the like can be given. Such a solid titanium catalyst component can be obtained by contacting a magnesium compound, a titanium compound, and, if necessary, an electron donor as described below.

<Magnesium compound>
Specific examples of the magnesium compound include magnesium halides such as magnesium chloride and magnesium bromide;
Alkoxy magnesium halides such as methoxy magnesium chloride, ethoxy magnesium chloride, phenoxy magnesium chloride;
Alkoxymagnesium such as ethoxymagnesium, isopropoxymagnesium, butoxymagnesium, 2-ethylhexoxymagnesium;
Aryloxymagnesium such as phenoxymagnesium;
Known magnesium compounds such as magnesium carboxylates such as magnesium stearate can be mentioned.

  These magnesium compounds may be used alone or in combination of two or more. These magnesium compounds may be complex compounds with other metals, double compounds, or mixtures with other metal compounds.

  Of these, magnesium compounds containing halogen are preferred. Magnesium halides, particularly magnesium chloride, are preferably used. In addition, alkoxymagnesium such as ethoxymagnesium is also preferably used. The magnesium compound may be derived from other substances, for example, obtained by contacting an organic magnesium compound such as a Grignard reagent with titanium halide, silicon halide, halogenated alcohol or the like. Good.

<Titanium compound>
Examples of titanium compounds include general formula (1);
Ti (OR) _g X _4-g (1)
(In general formula (1), R is a hydrocarbon group, X is a halogen atom, g is 0 <= g <= 4), The tetravalent titanium compound shown can be mentioned. More specifically,
Titanium tetrahalides such as TiCl ₄ and TiBr ₄ ;
Ti (OCH ₃ ) Cl ₃ , Ti (OC ₂ H ₅ ) Cl ₃ , Ti (O—n—C ₄ H ₉ ) Cl ₃ , Ti (OC ₂ H ₅
) Br ₃ , trihalogenated alkoxytitanium such as Ti (O—isoC ₄ H ₉ ) Br ₃ ;
Dihalogenated alkoxytitanium such as Ti (OCH ₃ ) ₂ Cl ₂ , Ti (OC ₂ H ₅ ) ₂ Cl ₂ ;
Monohalogenated alkoxytitanium such as Ti (OCH ₃ ) ₃ Cl, Ti (O—n—C ₄ H ₉ ) ₃ Cl, Ti (OC ₂ H ₅ ) ₃ Br;
Examples thereof include tetraalkoxytitanium such as Ti (OCH ₃ ) ₄ , Ti (OC ₂ H ₅ ) ₄ , Ti (OC ₄ H ₉ ) ₄ , and Ti (O-2-ethylhexyl) ₄ .
Among these, titanium tetrahalide is preferable, and titanium tetrachloride is particularly preferable. These titanium compounds may be used alone or in combination of two or more.

<Electron donor>
The solid titanium catalyst component [A] of the present invention may contain a known electron donor or a substitute thereof. Preferable examples of the electron donor include an electron donor selected from an aromatic carboxylic acid ester, an alicyclic carboxylic acid ester, a compound having two or more ether bonds via a plurality of carbon atoms, that is, a polyether compound ( a).

If the solid titanium catalyst component [A] of the present invention contains an electron donor, the molecular weight of the resulting polyolefin may be controlled to be high, or the molecular weight distribution may be controlled.
Specific examples of such aromatic carboxylic acid esters include aromatic polycarboxylic acid esters such as phthalic acid esters, in addition to aromatic carboxylic acid monoesters such as toluic acid esters. Among these, aromatic polycarboxylic acid esters are preferable, and phthalic acid esters are more preferable. As the phthalic acid esters, phthalic acid alkyl esters such as ethyl phthalate, n-butyl phthalate, isobutyl phthalate, hexyl phthalate, and heptyl phthalate are preferable, and diisobutyl phthalate is particularly preferable.

  More specifically, examples of the polyether compound include compounds represented by the following general formula (2).

In the general formula (2), m is an integer of 1 ≦ m ≦ 10, more preferably an integer of 3 ≦ m ≦ 10, and R ^{11 to} R ³⁶ are each independently a hydrogen atom, carbon, It is a substituent having at least one element selected from hydrogen, oxygen, fluorine, chlorine, bromine, iodine, nitrogen, sulfur, phosphorus, boron and silicon.

When m is 2 or more, a plurality of R ¹¹ and R ¹² may be the same or different. Arbitrary R ^{11 to} R ³⁶ , preferably R ¹¹ and R ¹² may jointly form a ring other than a benzene ring.

Some specific examples of such compounds include:
2,2-dicyclohexyl-1,3-dimethoxypropane,
2-methyl-2-isopropyl-1,3-dimethoxypropane,
2-cyclohexyl-2-methyl-1,3-dimethoxypropane,
2-isobutyl-2-methyl-1,3-dimethoxypropane,
2,2-diisobutyl-1,3-dimethoxypropane,
2,2-bis (cyclohexylmethyl) -1,3-dimethoxypropane,
2,2-diisobutyl-1,3-diethoxypropane,
2,2-diisobutyl-1,3-dibutoxypropane,
2,2-di-sec-butyl-1,3-dimethoxypropane,
2,2-dineopentyl-1,3-dimethoxypropane,
2-isobutyl-2-isopropyl-1,3-dimethoxypropane,
2-isopentyl-2-isopropyl-1,3-dimethoxypropane,
2-cyclohexyl-2-cyclohexylmethyl-1,3-dimethoxypropane,
2-methyl-2-n-propyl-1,3-diethoxypropane,
Disubstituted 2-alkoxypropanes such as 2, -2-diethyl-1,3-diethoxypropane
2-methoxymethyl-2-methyl-1,3-dimethoxypropane,
2-cyclohexyl-2-ethoxymethyl-1,3-diethoxypropane,
Trialkoxyalkanes such as 2-cyclohexyl-2-methoxymethyl-1,3-dimethoxypropane,
2,2-diisobutyl-1,3-dimethoxy-cyclohexane,
2-isoamyl-2-isopropyl-1,3-dimethoxycyclohexane,
2-cyclohexyl-2-methoxymethyl-1,3-dimethoxycyclohexane,
2-isopropyl-2-methoxymethyl-1,3-dimethoxycyclohexane,
2-isobutyl-2-methoxymethyl-1,3-dimethoxycyclohexane,
2-cyclohexyl-2-ethoxymethyl-1,3-dimethoxycyclohexane,
2-ethoxymethyl-2-isopropyl-1,3-dimethoxycyclohexane,
Examples thereof include dialkoxycycloalkanes such as 2-isobutyl-2-ethoxymethyl-1,3-dimethoxycyclohexane.

  Among these, 2-isobutyl-2-isopropyl-1,3-dimethoxypropane, 2,2-diisobutyl-1,3-dimethoxypropane, 2-isopentyl-2-isopropyl-1,3-dimethoxypropane, 2 , 2-dicyclohexyl-1,3-dimethoxypropane, 2,2-bis (cyclohexylmethyl) 1,3-dimethoxypropane, 2-methyl-2-n-propyl-1,3-diethoxypropane, 2,2- Diethyl-1,3-diethoxypropane is preferred.

These compounds may be used individually by 1 type, and may be used in combination of 2 or more type.
The alicyclic carboxylic acid ester compound is represented by the following general formula (3).

In General formula (3), n is an integer of 5-10, Preferably it is an integer of 5-7, Most preferably, it is 6. C ^a represents a carbon atom.

R ² and R ³ are each independently COOR ¹ or R, and at least one of R ² and R ³ is COOR ¹ .
It is preferable that all the bonds between carbon atoms in the cyclic skeleton are single bonds, but any single bond other than the C ^a -C ^a bond in the cyclic skeleton may be replaced with a double bond. .

A plurality of R ^{1 s} are each independently a monovalent carbon atom having 1 to 20, preferably 1 to 10, more preferably 2 to 8, still more preferably 4 to 8, particularly preferably 4 to 6 carbon atoms. It is a hydrogen group. As this hydrocarbon group, ethyl group, n-propyl group, isopropyl group, n-butyl group, isobutyl group, hexyl group, heptyl group, octyl group, 2-ethylhexyl group, decyl group, dodecyl group, tetradecyl group, A hexadecyl group, an octadecyl group, an eicosyl group, and the like can be mentioned. Among them, an n-butyl group, an isobutyl group, a hexyl group, and an octyl group are preferable, and an n-butyl group and an isobutyl group are more preferable.

  A plurality of R's are each independently an atom selected from a hydrogen atom, a hydrocarbon group having 1 to 20 carbon atoms, a halogen atom, a nitrogen-containing group, an oxygen-containing group, a phosphorus-containing group, a halogen-containing group and a silicon-containing group. Or a group.

  R is preferably a hydrocarbon group having 1 to 20 carbon atoms, and examples of the hydrocarbon group having 1 to 20 carbon atoms include a methyl group, an ethyl group, an n-propyl group, an iso-propyl group, and an n-butyl group. , Iso-butyl group, sec-butyl group, n-pentyl group, cyclopentyl group, n-hexyl group, cyclohexyl group, vinyl group, phenyl group, octyl group and other aliphatic hydrocarbon groups, alicyclic hydrocarbon groups, An aromatic hydrocarbon group is mentioned. Among them, an aliphatic hydrocarbon group is preferable, and specifically, a methyl group, an ethyl group, an n-propyl group, an iso-propyl group, an n-butyl group, an iso-butyl group, and a sec-butyl group are preferable.

R may be bonded to each other to form a ring, and a ring skeleton formed by bonding of R to each other may contain a double bond, and in the ring skeleton, When two or more C ^a bonded with COOR ¹ are contained, the number of carbon atoms constituting the ring skeleton is 5 to 10.
Examples of such a ring skeleton include a norbornane skeleton and a tetracyclododecene skeleton.

  A plurality of Rs may be a carbonyl structure-containing group such as a carboxylic acid ester group, an alkoxy group, a siloxy group, an aldehyde group or an acetyl group, and these substituents include one or more hydrocarbon groups. It is preferable that

As a preferable example of such an alicyclic ester compound,
3,6-dimethylcyclohexane-1,2-dicarboxylic acid ester,
Examples include 3-methyl-6-propylcyclohexane-1,2-dicarboxylic acid ester cyclohexane-1,2-dicarboxylic acid ester and the like.

The compound having the diester structure as described above has isomers such as cis and trans derived from a plurality of COOR ¹ groups in the general formula (3), and any structure is suitable for the purpose of the present invention. Has the effect of From the viewpoint of polymerization activity, the trans isomer content is particularly high.

  The solid titanium catalyst component used in the present invention, when used as a catalyst for olefin polymerization, has a high reactivity at the initial stage of the polymerization reaction and deactivates in a relatively short time (initially active type), and a reaction at the initial stage of the polymerization reaction The properties can be broadly classified into the types in which the reaction tends to be sustained even though they are mild (sustained activity type), but it is speculated that the latter sustained activity type is preferable as the solid titanium catalyst component of the present invention. This is because if the reactivity is too high, melting of the surface of the ethylene polymer particles as described above and fusion between the particles are likely to occur. From this viewpoint, among the aromatic carboxylic acid ester, alicyclic carboxylic acid ester, and ether compound, aromatic polyvalent ester, alicyclic polyvalent ester, and ether compound are preferable, and ether compound is more preferable. . Further, 1,3-diethers are preferred, and in particular, 2-isobutyl-2-isopropyl-1,3-dimethoxypropane, 2,2-diisobutyl-1,3-dimethoxypropane, 2-isopentyl-2-isopropyl-1 1,2-dimethoxypropane, 2,2-dicyclohexyl-1,3-dimethoxypropane and 2,2-bis (cyclohexylmethyl) 1,3-dimethoxypropane are preferred. The reason is unknown, but according to the results of experiments conducted by the present inventors, the solid titanium catalyst component containing the above 1,3-diether compound tends to give an ultrahigh molecular weight ethylene polymer having a high crystallinity. There is.

  These electron donors (a) such as aromatic carboxylic acid ester, alicyclic carboxylic acid ester and ether compound may be used alone or in combination of two or more. The electron donor may be formed in the process of preparing the solid titanium catalyst component [A]. Specifically, when an ester compound is taken as an example, when the solid titanium catalyst component [A] is prepared, the carboxylic anhydride or carboxylic dihalide corresponding to the ester substantially contacts with the corresponding alcohol. By providing the step, the ester compound can be contained in the solid titanium catalyst component.

For the preparation of the solid titanium catalyst component [A] used in the present invention, a known method can be used without limitation. Specific preferred methods include, for example, the following methods (P-1) to (P-4).
(P-1) A solid adduct composed of an electron donor such as a magnesium compound and alcohol, an electron donor (a), and a liquid state titanium compound are contacted in a suspended state in the presence of an inert hydrocarbon solvent. How to make.
(P-2) A method in which a solid adduct composed of an electron donor such as a magnesium compound and alcohol, an electron donor (a), and a titanium compound in a liquid state are contacted in a plurality of times.
(P-3) A solid adduct comprising an electron donor such as a magnesium compound and alcohol, an electron donor (a), and a liquid titanium compound in a suspended state in the presence of an inert hydrocarbon solvent. The method of making it contact and dividing in multiple times.
(P-4) A method of contacting a liquid magnesium compound comprising an electron donor such as a magnesium compound and alcohol, a liquid titanium compound, and the electron donor (a).

  The preferred reaction temperature is in the range of −30 ° C. to 150 ° C., more preferably −25 ° C. to 130 ° C., still more preferably −25 to 120 ° C.

  The production of the above solid titanium catalyst component can also be carried out in the presence of a known medium, if necessary. Examples of the medium include aromatic hydrocarbons such as slightly polar toluene and o-dichlorotoluene, and known aliphatic hydrocarbons such as heptane, octane, decane, and cyclohexane, and alicyclic hydrocarbon compounds. In these, an aliphatic hydrocarbon is mentioned as a preferable example.

  In the solid titanium catalyst component [A] used in the present invention, the halogen / titanium (atomic ratio) (that is, the number of moles of halogen atom / number of moles of titanium atom) is 2 to 100, preferably 4 to 90. It is desirable.

Magnesium / titanium (atomic ratio) (that is, the number of moles of magnesium atoms / the number of moles of titanium atoms) is 2 to 100, preferably 4 to 50.
The electron donor (a) / titanium (molar ratio) (that is, the number of moles of electron donor selected from aromatic carboxylic acid ester, alicyclic carboxylic acid ester, polyether compound / number of moles of titanium atom) is 0. It is desirable that it is -100, preferably 0.2-10.

[Organometallic compound catalyst component [B]]
The aforementioned olefin polymerization catalyst is:
The solid titanium catalyst component [A] according to the present invention,
And an organometallic compound catalyst component [B] containing a metal element selected from Group 1, Group 2 and Group 13 of the Periodic Table.
As the organometallic compound catalyst component [B], a compound containing a Group 13 metal, for example, an organoaluminum compound, a complex alkylated product of a Group 1 metal and aluminum, an organometallic compound of a Group 2 metal, or the like is used. it can. Among these, an organoaluminum compound is preferable.

Specific examples of the organometallic compound catalyst component [B] are described in detail in the aforementioned publicly known literature. Examples of such an organometallic compound catalyst component [B] include, for example, the general formula (4),
^{_{R a n AlX 3-n (}} 4)
(In general formula (4), R ^a is a hydrocarbon group having 1 to 12 carbon atoms, X is a halogen or hydrogen, and n is 1 ≦ n ≦ 3). can do. In the general formula (4), R ^a is a hydrocarbon group having 1 to 12 carbon atoms, such as an alkyl group, a cycloalkyl group, or an aryl group. Specifically, a methyl group, an ethyl group, n -Propyl group, isopropyl group, isobutyl group, pentyl group, hexyl group, octyl group, cyclopentyl group, cyclohexyl group, phenyl group, tolyl group and the like. Among these, trialkylaluminum with n = 3, particularly triethylaluminum, triisobutylaluminum and the like are preferable. These compounds can also be used as a mixture of two or more.

[Catalyst component [C]]
Moreover, the catalyst for olefin polymerization may contain the well-known catalyst component [C] as needed with said organometallic compound catalyst component [B]. The catalyst component [C] is preferably an organosilicon compound. Examples of the organosilicon compound include compounds represented by the following general formula (5).
R _n Si (OR ′) _4-n (5)

  In general formula (5), R and R ′ are hydrocarbon groups, and n is an integer of 0 <n <4. Preferable specific examples of the organosilicon compound represented by the general formula (5) are vinyltriethoxysilane, diphenyldimethoxysilane, dicyclohexyldimethoxysilane, cyclohexylmethyldimethoxysilane, and dicyclopentyldimethoxysilane.

A silane compound represented by the following general formula (6) described in International Publication No. 2004/016662 pamphlet is also a preferable example of the organosilicon compound.
Si (OR ^a ) ₃ (NR ^b R ^c ) (6)

In the general formula (6), R ^a is a hydrocarbon group having 1 to 6 carbon atoms, and examples of R ^a include an unsaturated or saturated aliphatic hydrocarbon group having 1 to 6 carbon atoms, Particularly preferred is a hydrocarbon group having 2 to 6 carbon atoms. Specific examples include methyl group, ethyl group, n-propyl group, iso-propyl group, n-butyl group, iso-butyl group, sec-butyl group, n-pentyl group, iso-pentyl group, cyclopentyl group, n- A hexyl group, a cyclohexyl group, etc. are mentioned, Among these, an ethyl group is particularly preferable.

In general formula (6), R ^b is a hydrocarbon group having 1 to 12 carbon atoms or hydrogen, and R ^b is an unsaturated or saturated aliphatic hydrocarbon group having 1 to 12 carbon atoms or hydrogen. Etc. Specific examples include a hydrogen atom, a methyl group, an ethyl group, an n-propyl group, an iso-propyl group, an n-butyl group, an iso-butyl group, a sec-butyl group, an n-pentyl group, an iso-pentyl group, and a cyclopentyl group. , N-hexyl group, cyclohexyl group, octyl group and the like, among which ethyl group is particularly preferable.

In general formula (6), R ^c is a hydrocarbon group having 1 to 12 carbon atoms, and R ^c is an unsaturated or saturated aliphatic hydrocarbon group having 1 to 12 carbon atoms or hydrogen. Can be mentioned. Specific examples include methyl group, ethyl group, n-propyl group, iso-propyl group, n-butyl group, iso-butyl group, sec-butyl group, n-pentyl group, iso-pentyl group, cyclopentyl group, n- A hexyl group, a cyclohexyl group, an octyl group, etc. are mentioned, Among these, an ethyl group is particularly preferable.

Specific examples of the compound represented by the general formula (6) include
Dimethylaminotriethoxysilane,
Diethylaminotriethoxysilane,
Diethylaminotrimethoxysilane,
Diethylaminotriethoxysilane,
Diethylaminotri-n-propoxysilane,
Di-n-propylaminotriethoxysilane,
Methyl n-propylaminotriethoxysilane,
t-butylaminotriethoxysilane,
Ethyl n-propylaminotriethoxysilane,
Ethyl iso-propylaminotriethoxysilane,
Mention may be made of methylethylaminotriethoxysilane.

  Other useful compounds as the catalyst component [C] include the aromatic carboxylic acid ester, alicyclic carboxylic acid ester and / or plural compounds that can be used in the preparation of the solid titanium catalyst component [A]. A polyether compound described as an example of a compound having two or more ether bonds via the carbon atom is also preferable.

  Among these polyether compounds, 1,3-diethers are preferable, and 2-isobutyl-2-isopropyl-1,3-dimethoxypropane, 2,2-diisobutyl-1,3-dimethoxypropane, 2-isopentyl are particularly preferable. -2-isopropyl-1,3-dimethoxypropane, 2,2-dicyclohexyl-1,3-dimethoxypropane, 2,2-bis (cyclohexylmethyl) 1,3-dimethoxypropane, 2-methyl-2-n-propyl 1,3-diethoxypropane and 2, -2-diethyl-1,3-diethoxypropane are preferred.

  These catalyst components [C] can be used alone or in combination of two or more.

  In addition to these, olefin polymerization catalysts that can be used in the present invention include metallocene compounds disclosed in JP-A No. 2004-168744, JP-A No. 2000-128931, and JP-A No. 2004-646097. Olefin polymerization catalyst comprising an organometallic complex having a phenoxyimine compound or the like as a ligand and an organometallic compound catalyst component as disclosed in JP, No. 2005-2244, JP-A No. 2005-2086, etc. Can also be exemplified as a preferred catalyst for olefin polymerization.

  The olefin polymerization catalyst of the present invention may contain other components useful for olefin polymerization as necessary in addition to the above components. Examples of other components include metal oxides such as silica, which are mainly used as carriers, antistatic agents, particle aggregating agents, storage stabilizers, and the like.

[Method for Producing Ethylene Polymer Particles] The method for producing ethylene polymer particles according to the present invention is characterized in that olefins containing ethylene are polymerized using the olefin polymerization catalyst of the present invention. In the present invention, “polymerization” may include the meaning of copolymerization such as random copolymerization and block copolymerization in addition to homopolymerization.

  In the method for producing ethylene polymer particles of the present invention, the polymerization is carried out in the presence of a prepolymerization catalyst obtained by prepolymerization of an α-olefin in the presence of the olefin polymerization catalyst of the present invention. It is also possible to do this. This prepolymerization is carried out by prepolymerizing α-olefin in an amount of 0.1 to 1000 g, preferably 0.3 to 500 g, particularly preferably 1 to 200 g, per 1 g of the solid catalyst component contained in the olefin polymerization catalyst. Is called.

In the prepolymerization, a catalyst having a higher concentration than the catalyst concentration in the system in the main polymerization can be used.
The concentration of the solid titanium catalyst component [A] in the prepolymerization is usually 0.001 to 200 mmol, preferably 0.01 to 50 mmol, particularly preferably 0, in terms of titanium atom, per liter of the liquid medium. Desirably, the range is from 1 mmol to 20 mmol.

  The amount of the organometallic compound catalyst component [B] in the prepolymerization is such that 0.1 g to 1000 g, preferably 0.3 g to 500 g of a polymer is produced per 1 g of the solid titanium catalyst component [A]. The amount is usually 0.1 mol to 300 mol, preferably 0.5 mol to 100 mol, particularly preferably 1 mol to 50 mol, per mol of titanium atom in the solid titanium catalyst component [A]. It is desirable.

  In the prepolymerization, the catalyst component [C] or the like can be used as necessary. In this case, these components are used in an amount of 0.1 mol to 1 mol of titanium atom in the solid titanium catalyst component [A]. It is used in an amount of 50 mol, preferably 0.5 mol to 30 mol, more preferably 1 mol to 10 mol.

  The prepolymerization can be performed under mild conditions by adding an olefin and the above catalyst components to an inert hydrocarbon medium.

In this case, specific examples of the inert hydrocarbon medium used include aliphatic hydrocarbons such as propane, butane, pentane, hexane, heptane, octane, decane, dodecane, and kerosene;
Cycloaliphatic hydrocarbons such as cycloheptane, methylcycloheptane, cyclohexane, methylcyclohexane, methylcyclopentane, cyclooctane, methylcyclooctane;
Aromatic hydrocarbons such as benzene, toluene, xylene;
Halogenated hydrocarbons such as ethylene chloride and chlorobenzene,
Alternatively, a mixture thereof can be used.

  Of these inert hydrocarbon media, it is particularly preferable to use aliphatic hydrocarbons. Thus, when using an inert hydrocarbon medium, it is preferable to perform prepolymerization by a batch type.

  On the other hand, the prepolymerization can be carried out using the olefin itself as a solvent, or the prepolymerization can be carried out in a substantially solvent-free state. In this case, it is preferable to perform preliminary polymerization continuously.

The olefin used in the prepolymerization may be the same as or different from the olefin used in the main polymerization described later. Specifically, ethylene and propylene are preferable.
The temperature during the prepolymerization is usually −20 to + 100 ° C., preferably −20 to + 80 ° C., more preferably 0 to + 40 ° C.
Next, the main polymerization carried out after passing through the pre-polymerization or without going through the pre-polymerization will be described.

  In the main polymerization, ethylene is polymerized in the presence of the olefin polymerization catalyst. In addition to ethylene, an α-olefin having 3 to 20 carbon atoms such as propylene, 1-butene, 1-pentene, 1-hexene, 1-octene, 1-decene, 1-dodecene, 1-tetradecene, 1- Even if linear olefins such as hexadecene, 1-octadecene, 1-eicosene, and branched olefins such as 4-methyl-1-pentene, 3-methyl-1-pentene, and 3-methyl-1-butene are shared good. These α-olefins are preferably propylene, 1-butene, 1-pentene and 4-methyl-1-pentene.

  Along with these α-olefins, aromatic vinyl compounds such as styrene and allylbenzene; alicyclic vinyl compounds such as vinylcyclohexane and vinylcycloheptane can also be used.

In the present invention, the prepolymerization and the main polymerization can be performed by any of a liquid phase polymerization method such as a bulk polymerization method, a solution polymerization and a suspension polymerization, or a gas phase polymerization method.
When the main polymerization takes the form of slurry polymerization, the reaction solvent can be an inert hydrocarbon used during the above-mentioned prepolymerization, or an olefin that is liquid at the reaction temperature.

  In the main polymerization in the polymerization method of the present invention, the solid titanium catalyst component [A] is usually 0.0001 to 0.5 mmol, preferably 0.5, in terms of titanium atoms per liter of polymerization volume. Used in an amount of 005 mmol to 0.1 mmol. The organometallic compound catalyst component [B] is usually in an amount of 1 mol to 2000 mol, preferably 5 mol to 500 mol, per 1 mol of titanium atom in the prepolymerization catalyst component in the polymerization system. Used. When the catalyst component [C] is used, it is 0.001 to 50 mol, preferably 0.01 to 30 mol, particularly preferably 0.05 mol, relative to the organometallic compound catalyst component [B]. Used in an amount of ˜20 mol.

  If the main polymerization is carried out in the presence of hydrogen, the molecular weight of the resulting polymer can be adjusted. In particular, when the ultra high molecular weight ethylene polymer particles of the present invention are produced, it is preferable to polymerize ethylene in the presence of hydrogen. The reason for this is not clear at the present time, but by performing polymerization in the presence of hydrogen, chain transfer reaction by olefins such as ethylene is suppressed, and ultrahigh molecular weight ethylene polymer particles having a structure of saturated bonds at the molecular ends, That is, it is presumed that a stable ultra-high molecular weight ethylene polymer that hardly changes in quality during molding can be obtained.

In the main polymerization in the present invention, the polymerization temperature of the olefin is usually 20 ° C to 200 ° C, preferably 30 ° C to 100 ° C, more preferably 50 ° C to 90 ° C. The pressure is usually set to normal pressure to 10 MPa, preferably 0.20 MPa to 5 MPa. In the polymerization method of the present invention, the polymerization can be carried out by any of batch, semi-continuous and continuous methods. Furthermore, the polymerization can be carried out in two or more stages by changing the reaction conditions. In particular,
(A) Intrinsic viscosity [η] is 2 dl / g or more and less than 10 dl / g, preferably [η] is 3 dl / g or more and less than 10 dl / g, more preferably [η] is 5 dl / g or more and 10 dl / g. Producing less than ethylene polymer, and
(B) Intrinsic viscosity [η] is 5 dl / g or more and 35 dl / g or less, preferably [η] is 7 dl / g or more and 33 dl / g or less, more preferably [η] is 10 dl / g or more and 33 dl / g. Hereinafter, it is particularly preferable to produce the ethylene polymer under conditions including a step of producing an ethylene polymer having [η] of 15 dl / g or more and 32 dl / g or less. However, the intrinsic viscosity [η] of the polymer obtained in the step (a) is different from the [η] of the polymer obtained in the step (b), and further, the intrinsic viscosity of the polymer obtained in the step (a) [ [η] of the polymer obtained in step (b) is preferably higher than [η]. Furthermore, it is more preferable to carry out under the condition that [η] of the ethylene polymer produced in the first stage is lower than the intrinsic viscosity [η] of all ethylene polymers produced in the second stage and thereafter. That is, it is preferable that [η] of the ethylene polymer produced in the first stage is lower than the intrinsic viscosity [η] of the finally obtained ethylene polymer. The preferred range of the intrinsic viscosity [η] of the ethylene polymer produced in the first stage is the same as the [η] range of the ethylene polymer obtained in the step (a).

  The mass ratio of the ethylene polymer produced in the step (a) and the ethylene polymer produced in the step (b) depends on the intrinsic viscosity produced in each step, but the ethylene produced in the step a. The proportion of the polymer is 0 to 50% by mass, the proportion of the ethylene polymer produced in the step b is 100 to 50% by mass, and the ethylene polymer produced in the step a and the ethylene weight produced in the step b. The preferable mass ratio of the coalescence is 5/95 to 50/50, more preferably 10/90 to 40/60, and still more preferably 15/85 to 40/60. This mass ratio is determined by measuring the amount of ethylene absorbed in each step, sampling a small amount and a specified amount of the resin obtained in each step, and determining the mass, slurry concentration, catalyst component content in the resin, etc. It can be determined by calculating the amount of resin produced.

  When a polymerization reaction of ethylene or other olefin used as necessary is performed by a catalyst containing a solid titanium catalyst component, the polymerization reaction occurs at a catalytic active point in the solid titanium catalyst component. It is presumed that the polymer produced in the early stage of the polymerization reaction is unevenly distributed on the surface of the particle, and the polymer produced in the later stage of the polymerization reaction is unevenly distributed in the particle. This phenomenon is thought to be similar to the tree rings. Therefore, when the ethylene polymer is produced by dividing the reaction conditions into two or more stages in the present invention, the intrinsic viscosity [η] of the ethylene polymer produced in the first stage is [η] of the ethylene polymer finally obtained. If the production is performed under a lower condition, there is a high possibility that a polymer having a relatively low molecular weight is present on the particle surface, and it is considered that the particles are easily pressure-bonded during solid-phase stretch molding.

  The ethylene polymer particles of the present invention can be produced by a known polymerization method such as a batch type or a continuous type. When producing by the multistage polymerization process as described above, it is preferable to adopt a batch system. The ethylene polymer particles obtained by the batch type process are considered to be advantageous by the pressure bonding between the above-mentioned particles because there is little variation in the ethylene polymer obtained in the a step and the b step for each particle.

  The ultrahigh molecular weight ethylene polymer particles thus obtained may be any of a homopolymer, a random copolymer and a block copolymer. The ethylene polymer particles of the present invention are preferably ethylene homopolymers from the viewpoint of easily obtaining a polymer having a high degree of crystallinity.

  The ultrahigh molecular weight ethylene polymer particles of the present invention may be particles themselves obtained by polymerizing ethylene in the presence of the olefin polymerization catalyst as described above. It is preferable to pass through the process of hold | maintaining to the temperature below degree C and below melting | fusing point. Specific conditions include 100 ° C. to 140 ° C., preferably 105 ° C. to 140 ° C., more preferably 110 ° C. to 135 ° C., 15 minutes to 24 hours, preferably 1 to 10 hours, more preferably 1 to 10 hours. The condition of 4 hours can be mentioned. Specific methods include a method of maintaining the ethylene polymer particles obtained by polymerization under the above conditions using an oven or the like, or a step after the polymerization reaction, for example, drying, in the production process of the ethylene polymer particles. The method etc. which perform a process etc. on said conditions are mentioned. By passing through such a process, ultra high molecular weight ethylene polymer particles having a higher crystallinity can be obtained.

  In a liquid phase atmosphere, it is 90 ° C to 140 ° C, preferably 95 ° C to 140 ° C, more preferably 95 ° C to 135 ° C, and further 95 ° C to 130 ° C for 15 minutes to 24 hours, preferably 1 to Ethylene polymer particles obtained through a process under conditions of 10 hours, more preferably 1 to 4 hours are preferred.

  The ultra high molecular weight ethylene polymer molded product of the present invention can be obtained by molding the above ultra high molecular weight ethylene polymer particles by a known molding method for ultra high molecular weight polyethylene. Since the molded product of the present invention uses an ultra-high molecular weight ethylene polymer having a high degree of crystallinity, it tends to be excellent in strength. Further, when an ethylene polymer obtained by a multistage polymerization method is used, the moldability tends to be excellent, and therefore, the degree of freedom of shape of the molded product is expected to be higher than that of the conventional one. Among the molded products of the present invention, a molded product obtained by a solid phase stretching method is particularly preferable.

As the conditions for solid-phase stretch molding, known conditions described in Patent Documents 3 to 5 can be used without limitation, except that the above ultrahigh molecular weight ethylene polymer particles are used. For example, there is a method in which the ethylene polymer particles of the present invention are pressure-bonded at a pressure of 10 MPa or more and formed into a sheet shape, and this is stretched at a relatively high temperature or stretched while applying pressure using a roll or the like. It is done. The temperature during the molding is preferably not higher than the melting point of the ethylene polymer particles, but if the melt flow does not substantially occur, the molding may be performed at the melting point or higher.
The stretchability of a molded product using the ethylene polymer particles of the present invention and the physical properties of the stretched molded product can be evaluated by the following methods.

(Stretch ratio)
The ethylene polymer particles are pressed at a temperature of 136 ° C. and a pressure of 15.2 MPa for 30 minutes to produce a sheet having a thickness of about 500 μm and cut into a shape of 35 mm length × 7 mm width.
Separately, a cylindrical high-density polyethylene molded product having a convex tapered shape at the tip is prepared, and this molded product is halved along the central axis (hereinafter referred to as billet).
The above cut out sheet is fixed by being sandwiched between flat portions of the billet.

The billet in this state is compressed and stretched by passing it through a concave taper-shaped nozzle heated to 120 ° C. at a speed of 1 cm / min. The convex taper shape of the nozzle and the concave taper shape of the billet are shapes in which the irregularities match.
The ratio of the respective cross-sectional areas at the inlet and outlet of the nozzle is 6: 1, and the sheet is stretched 6 times in the longitudinal direction.

(Preliminary stretching)
Next, the stretched sheet obtained by the above pre-stretching is cut out and set in a tensile tester (manufactured by Instron Co., Ltd., universal testing machine 55R1122) so that the distance between chucks is 9 mm. Uniaxial stretching is performed at a temperature of 135 ° C. and a tensile speed of 18 mm / min until fracture occurs in the same direction as the preliminary stretching.
A value obtained by multiplying the second draw ratio by 6 times in the preliminary drawing is evaluated as the draw ratio for the evaluation.

(Physical properties)
Based on the ASTM standard, the tensile strength and tensile elastic modulus of the stretched molded product can be measured using a tensile tester (manufactured by Instron Co., Ltd., universal testing machine 55R1122 type).

  When the ethylene polymer of the present invention is used, a high performance with the draw ratio of 90 times or more can be obtained. More preferably, it is 90 times to 500 times, still more preferably 100 times to 400 times, particularly preferably 120 times to 350 times, and particularly preferably 140 times to 350 times.

  It is generally known to those skilled in the art that the higher the draw ratio, the higher the strength of the stretched molded product. That is, if the draw ratio is increased, it is advantageous to obtain a high-strength yarn or sheet.

  Since the solid phase stretch molded product of the present invention can be molded at a high draw ratio, it is expected to have high strength. In addition, since solid-phase stretch molding is a method that does not use a solvent, the molding equipment is relatively simple, and it is a molding method that has little negative impact on the environment, and is expected to have a high contribution to society. .

Next, although this invention is demonstrated based on an Example, it cannot be overemphasized that this invention is not limited to the following Example, unless it deviates from the summary.
In the following examples, the intrinsic viscosity [η], crystallinity, and particle surface shape of ultrahigh molecular weight ethylene polymer particles were measured by the following methods.

(Intrinsic viscosity [η])
The intrinsic viscosity [η] was measured in decalin at a temperature of 135 ° C. by dissolving ultrahigh molecular weight ethylene polymer particles in decalin.

(Crystallinity)
The crystallinity was measured by the wide-angle X-ray diffraction transmission method with the following apparatus and conditions.
X-ray crystal analyzer: Rigaku Corporation RINT2500 type device X-ray source: CuKα
Output: 50KV, 300mA
Detector: Scintillation counter Sample: The obtained polymer particles were used as they were.

Specifically, about 0.002 g of polymer particles were placed on a rotating sample stage installed in a RINT 2500 type apparatus manufactured by Rigaku Corporation, and wide-angle X-ray diffraction transmission measurement was performed while rotating the sample stage at 77 rpm. .
The crystallinity was calculated from the obtained wide-angle X-ray diffraction profile.

(SEM observation)
A sample stage with a diameter of about 1 centimeter of a JSM-6300F scanning electron microscope manufactured by JEOL was filled with the ethylene polymer particles, and the sample was observed with an SEM at room temperature to obtain a photograph magnified 2000 times. From the photograph, confirmation of the presence or absence of the thread-like structure and the thickness and length of the thread-like structure were measured.

(Average particle diameter and ratio of particles having a particle diameter of 355 μm or more)
Seven types of sieves having an opening diameter of 45 μm to 850 μm were used to classify 5 g of ethylene polymer particles mixed with a very small amount of carbon black as an antistatic agent.
Based on the result, the median diameter was determined by a conventional method to calculate the average particle diameter.

  On the other hand, as for the ratio of particles having a particle size of 355 μm or more, classification is performed in the same manner as described above except that a sieve having an opening diameter of 355 μm is used. Calculated. If a sieve having an aperture size of 355 μm is used for classification in the above average particle size calculation method, the average particle size and the ratio of particles having a particle size of 355 μm or more can be measured at a time.

(Stretch ratio)
The ethylene polymer particles are pressed at a temperature of 136 ° C. and a pressure of 15.2 MPa for 30 minutes to produce a sheet having a thickness of about 500 μm and cut into a shape of 35 mm length × 7 mm width.

Separately, a cylindrical high-density polyethylene molded product having a convex tapered shape at the tip is prepared, and this molded product is halved along the central axis (hereinafter referred to as billet).
The above cut out sheet is fixed by being sandwiched between flat portions of the billet.

The billet in this state is compressed and stretched by passing it through a concave taper-shaped nozzle heated to 120 ° C. at a speed of 1 cm / min. The convex taper shape of the nozzle and the concave taper shape of the billet are shapes in which the irregularities match.
The ratio of the respective cross-sectional areas at the inlet and outlet of the nozzle is 6: 1, and the sheet is stretched 6 times in the longitudinal direction.

(Preliminary stretching)
Next, the stretched sheet obtained by the above pre-stretching is cut out and set in a tensile tester (manufactured by Instron Co., Ltd., universal testing machine 55R1122) so that the distance between chucks is 9 mm. Uniaxial stretching is performed at a temperature of 135 ° C. and a tensile speed of 18 mm / min until breakage occurs in the same direction as the pre-stretching (the stretching ratio that can be measured under the above conditions is about 33 times at the maximum). The measurement was performed 3 to 5 times, and the highest value was taken as the value of the draw ratio.

A value obtained by multiplying the second draw ratio by 6 times in the preliminary drawing is evaluated as the draw ratio for the evaluation (therefore, the maximum draw ratio that can be measured in the evaluation publication is about 200 times).
).

[Example 1]
(Preparation of solid titanium catalyst component [A1])
Anhydrous magnesium chloride (75 g), decane (280.3 g) and 2-ethylhexyl alcohol (308.3 g) were heated and reacted at 130 ° C. for 3 hours to obtain a homogeneous solution, and 2-isobutyl-2-isopropyl-1,3 was then added to the solution. -19.9 g of dimethoxypropane was added and further stirred and mixed at 100 ° C for 1 hour.

  The homogeneous solution thus obtained was cooled to room temperature, and then 30 ml of this homogeneous solution was dropped into 80 ml of titanium tetrachloride maintained at −20 ° C. over 45 minutes with stirring. After the completion of charging, the temperature of the mixed solution was raised to 110 ° C. over 6 hours. When the temperature reached 110 ° C., 0.55 g of 2-isobutyl-2-isopropyl-1,3-dimethoxypropane was added to the mixed solution. Added and held under stirring at the same temperature for 2 hours. After the completion of the reaction for 2 hours, the solid part was collected by hot filtration, and the solid part was resuspended in 100 ml of titanium tetrachloride, and then heated again at 110 ° C. for 2 hours. After completion of the reaction, the solid part was again collected by hot filtration, and washed thoroughly with decane and hexane at a temperature of 90 ° C. until no free titanium compound was detected in the washing solution. The solid titanium catalyst component prepared by the above operation was stored as a decane slurry, but a part of the catalyst was dried for the purpose of examining the catalyst composition. The composition of the solid titanium catalyst component [A1] thus obtained was 2.8% by mass of titanium, 17% by mass of magnesium, 58% by mass of chlorine, 2-isobutyl-2-isopropyl-1,3-dimethoxypropane 19 0.5% by mass and 1.2% by mass of 2-ethylhexyl alcohol residue.

(polymerization)
Into a 1 liter polymerization vessel sufficiently purged with nitrogen, 500 ml of purified heptane was charged at room temperature. Under an ethylene atmosphere at a temperature of 78 ° C., 0.5 mmol of triisobutylaluminum as the organometallic compound catalyst component [B1] In addition, 0.005 mmol of solid titanium catalyst component [A1] was added in terms of titanium atoms. Next, 25 ml of hydrogen was added, ethylene was fed at a constant rate of 0.4 l / min, and ethylene polymerization was carried out at a temperature of 80 ° C. for 2.5 hours. The pressure during the polymerization rose to 0.46 MPa as a gauge pressure. After completion of the polymerization, the slurry containing the produced solid was filtered, dried under reduced pressure at a temperature of 80 ° C. overnight, and further maintained at a temperature of 120 ° C. for 3 hours. Further, it was passed through a sieve having an opening of 355 μm to remove particles having a particle size of 355 μm or more. The obtained ethylene polymer particles had an intrinsic viscosity [η] of 18.5 dl / g, a crystallinity of 83%, an average particle size of 200 μm, and a polymerization activity of 20,600 g / mmol-Ti. The inclusion of particles having a particle size of 355 μm or more was not recognized.

By SEM observation, it was confirmed that a large number of thread-like shapes having a thickness of 0.3 μm to 0.5 μm and a length of 3 μm to 10 μm existed on the surface of the obtained ethylene polymer particles. An SEM photograph of the surface of one particle is shown in FIG.
The above ethylene polymer particles were pressure-bonded at a temperature of 130 ° C. to prepare a sheet, and then stretched several times in an atmosphere at a temperature of 125 ° C. The sheet was not damaged.
Furthermore, the draw ratio was measured and a result of 99 times was obtained.

[Example 2]
(polymerization)
First step: 500 ml of purified heptane was charged at room temperature into a 1 liter polymerization vessel sufficiently purged with nitrogen, and triisobutylaluminum with an organometallic compound catalyst component [B1] at an temperature of 78 ° C. in an ethylene atmosphere. 0.5 mmol and 0.005 mmol of solid titanium catalyst component [A1] in terms of titanium atom were added. Then, after adding 75 ml of hydrogen, ethylene was fed at a constant rate of 0.4 l / min, and ethylene polymerization was carried out at a temperature of 80 ° C. for 1 hour. At this time, 10 ml of slurry was extracted from the polymerization vessel, and the intrinsic viscosity [η] of the white solid obtained by filtration and drying was measured and found to be 8.5 dl / g.

Second step: After completion of the above polymerization, ethylene and hydrogen were once purged to return to normal pressure. Next, 10 ml of hydrogen was introduced, ethylene was fed at a constant rate of 0.4 l / min, and ethylene was polymerized at 80 ° C. for 105 minutes.
After completion of the polymerization, the slurry containing the produced solid was filtered, dried under reduced pressure at 80 ° C. overnight, and further maintained at 130 ° C. for 3 hours.
Further, it was passed through a sieve having an opening of 355 μm to remove particles having a particle size of 355 μm or more.

  The obtained ethylene polymer particles had an intrinsic viscosity [η] of 23.6 dl / g, a crystallinity of 83%, an average particle size of 210 μm, and a polymerization activity of 22,200 g / mmol-Ti. The inclusion of particles having a particle size of 355 μm or more was not recognized. Further, the mass of the ethylene polymer obtained above, the mass of the ethylene polymer particles sampled in the first step, and the ratio of the polymerization amount in the first step and the second step determined from the slurry concentration are the first step / first step. 2 steps = 3/7 mass ratio. The intrinsic viscosity [η] of the polymer produced in the second step determined from these results was 30.1 dl / g.

Moreover, it was confirmed by SEM observation that a large number of thread-like shapes having a thickness of 0.3 μm to 0.5 μm and a length of 3 μm to 10 μm existed on the surface of the obtained ethylene polymer particles.
The above ethylene polymer particles were pressure-bonded at a temperature of 130 ° C. to prepare a sheet, and then stretched several times in an atmosphere at a temperature of 125 ° C. The sheet was not damaged.
Furthermore, when the stretch ratio was measured, a result of 193 times was obtained.

[Example 3]
(polymerization)
Polymerization was carried out in the same manner as in Example 2 except that 150 ml of hydrogen in the first step and the polymerization time were 48 minutes, 20 ml of hydrogen in the second step and 110 minutes of polymerization time were used. Further, it was passed through a sieve having an opening of 355 μm to remove particles having a particle size of 355 μm or more.

  The obtained ethylene polymer particles had an intrinsic viscosity [η] of 22.2 dl / g, a crystallinity of 83%, an average particle size of 200 μm, and a polymerization activity of 19,900 g / mmol-Ti. The inclusion of particles having a particle size of 355 μm or more was not recognized.

Further, the intrinsic viscosity [η] of the polymer obtained in the first step is 6.3 dl / g, and the ratio of the polymerization amount in the first step and the second step is the first step / second step = 2/8 mass. The intrinsic viscosity [η] of the polymer produced in the second step was 26.2 dl / g.
Moreover, it was confirmed by SEM observation that a large number of thread-like shapes having a thickness of 0.3 μm to 0.5 μm and a length of 3 μm to 10 μm existed on the surface of the obtained ethylene polymer particles.

The above ethylene polymer particles were pressure-bonded at a temperature of 130 ° C. to prepare a sheet, and then stretched several times in an atmosphere at a temperature of 125 ° C. The sheet was not damaged.
Further, when the stretching ratio was measured, no breakage of the sheet was observed in stretching up to 200 times.

[Example 4]
(polymerization)
Polymerization was carried out in the same manner as in Example 2 except that 150 ml of hydrogen in the first step, 53 minutes of polymerization time, 10 ml of hydrogen in the second step, and 107 minutes of polymerization time were used. Further, it was passed through a sieve having an opening of 355 μm to remove particles having a particle size of 355 μm or more.

  The obtained ethylene polymer particles had [η] of 21.9 dl / g, crystallinity of 83%, average particle size of 200 μm, and polymerization activity of 19,800 g / mmol-Ti. The inclusion of particles having a particle size of 355 μm or more was not recognized.

Further, the intrinsic viscosity [η] of the polymer obtained in the first step is 5.0 dl / g, and the ratio of the polymerization amount in the first step and the second step is the first step / second step = 3/7 mass. The intrinsic viscosity [η] of the polymer produced in the second step was 29.1 dl / g.
Moreover, it was confirmed by SEM observation that a large number of thread-like shapes having a thickness of 0.3 μm to 0.5 μm and a length of 3 μm to 10 μm existed on the surface of the obtained ethylene polymer particles.

The above ethylene polymer particles were pressure-bonded at a temperature of 130 ° C. to prepare a sheet, and then stretched several times in an atmosphere at a temperature of 125 ° C. The sheet was not damaged.
Further, when the stretching ratio was measured, no breakage of the sheet was observed in stretching up to 200 times.

[Example 5]
(polymerization)
Polymerization was carried out in the same manner as in Example 2 except that 300 ml of hydrogen in the first step, 55 minutes of polymerization time, 10 ml of hydrogen in the second step, and 130 minutes of polymerization time were used. Further, it was passed through a sieve having an opening of 355 μm to remove particles having a particle size of 355 μm or more.

  The obtained ethylene polymer particles had an intrinsic viscosity [η] of 21.0 dl / g, a crystallinity of 84%, an average particle size of 190 μm, and a polymerization activity of 18,800 g / mmol-Ti. The inclusion of particles having a particle size of 355 μm or more was not recognized.

In addition, the intrinsic viscosity [η] of the polymer obtained in the first step is 2.9 dl / g, and the ratio of the polymerization amount in the first step and the second step is the first step / second step = 2/8 mass. The intrinsic viscosity [η] of the polymer produced in the second step was 25.5 dl / g.
Further, it was confirmed by SEM observation that the obtained ethylene polymer particle surface had a large number of thread-like shapes mainly having a thickness of 0.3 μm to 0.5 μm and a length of 3 μm to 10 μm.

The above ethylene polymer particles were pressure-bonded at a temperature of 130 ° C. to prepare a sheet, and then stretched several times in an atmosphere at a temperature of 125 ° C. The sheet was not damaged.
Furthermore, the stretch ratio was measured, and a result of 173 times was obtained.

[Example 6]
(polymerization)
Polymerization was carried out under the same conditions as in Example 3 except that the amount of hydrogen used in the second stage was 15 ml. In addition, a 378 μm sieve was used instead of a 355 μm sieve.

  The draw ratio was more than 200 times, and the proportion of particles having a particle size of 355 μm or more was 1.8% by mass of the whole particles.

On the surface of the sheet obtained by the pre-stretching, there was a spot where the unevenness could be confirmed slightly visually. When the second stretch after the pre-stretching was performed with the sample obtained by cutting out the uneven portion, a phenomenon was observed in which the measurement sample was broken at a magnification of 10 times or less (total stretching magnification of 60 times or less).
In addition, said 200-times measurement result is a measured value of the site | part in which surface unevenness | corrugation is not observed visually.
The results are shown in Table 1.

[Example 7]
(polymerization)
Polymerization was performed under the same conditions as in Example 3. In addition, a 378 μm sieve was used instead of a 355 μm sieve.

  The draw ratio was more than 200 times, and the proportion of particles having a particle size of 355 μm or more was 4.4% by mass of the whole particles.

On the surface of the sheet obtained by pre-stretching, a relatively large number of spots where irregularities could be confirmed visually were observed. When the second stretching after the pre-stretching was performed with the sample from which the uneven portion was cut, a phenomenon was observed in which the measurement sample was broken in a stretching step of 10 times or less (total stretching ratio is 60 times or less).
In addition, said 200-times measurement result is a measured value of the site | part in which surface unevenness | corrugation is not observed visually.
The results are shown in Table 1.

[Example 8]
(polymerization)
Polymerization was carried out under the same conditions as in Example 4. In addition, a 378 μm sieve was used instead of a 355 μm sieve.

  The draw ratio was more than 200 times, and the proportion of particles having a particle size of 355 μm or more was 6.0% by mass of the whole particles.

On the surface of the sheet obtained by pre-stretching, a relatively large number of spots where irregularities could be confirmed visually were observed. When the second stretch after the pre-stretching was performed with the sample obtained by cutting out the uneven portion, a phenomenon was observed in which the measurement sample was broken at a magnification of 10 times or less (total stretching magnification of 60 times or less).
In addition, said 200-times measurement result is a measured value of the site | part in which surface unevenness | corrugation is not observed visually.
The results are shown in Table 1.

[Comparative Example 1]
(Preparation of solid titanium catalyst component [A2])
An anhydrous magnesium chloride 95.2 g, decane 398.4 g and 2-ethylhexyl alcohol 306 g were heated and reacted at a temperature of 140 ° C. for 6 hours to obtain a homogeneous solution, and 17.6 g of ethyl benzoate was added to the solution. The mixture was further stirred and mixed at 130 ° C. for 1 hour.

  The homogeneous solution thus obtained was cooled to room temperature, and then 50 ml of this homogeneous solution was dropped into 200 ml of titanium tetrachloride maintained at 0 ° C. over 1 hour with stirring. After the completion of charging, the temperature of the mixed solution was raised to 80 ° C. over 2.5 hours. When the temperature reached 80 ° C., 2.35 g of ethyl benzoate was added to the mixed solution, and the mixture was kept at the same temperature for 2 hours. Hold under stirring. After completion of the reaction for 2 hours, the solid part was collected by hot filtration, and the solid part was resuspended in 100 ml of titanium tetrachloride, and then heated at 90 ° C. for 2 hours. After completion of the reaction, the solid part was again collected by hot filtration, and washed thoroughly with decane and hexane at a temperature of 90 ° C. until no free titanium compound was detected in the washing solution. The solid titanium catalyst component [A2] prepared by the above operation was stored as a decant slurry.

(polymerization)
A polymerization vessel having an internal volume of 1 liter, which was sufficiently purged with nitrogen, was charged with 500 ml of purified heptane at room temperature, and in an ethylene atmosphere at a temperature of 78 ° C., triisobutylaluminum 0.5 as an organometallic compound catalyst component [B1]. 0.004 mmol of mmol and solid titanium catalyst component [A2] was added in terms of titanium atoms. Next, after raising the temperature to 80 ° C., ethylene polymerization was carried out for 55 minutes. The pressure during polymerization was maintained at 0.8 MPa as a gauge pressure. After completion of the polymerization, the slurry containing the purified solid was filtered and dried under reduced pressure at 80 ° C. overnight. Further, it was passed through a sieve having an opening of 355 μm to remove particles having a particle size of 355 μm or more.

The resulting ethylene polymer particles had an intrinsic viscosity [η] of 18.6 dl / g, a crystallinity of 77%, an average particle size of 180 μm, and a polymerization activity of 32,000 g / mmol-Ti. The inclusion of particles having a particle size of 355 μm or more was not recognized.
SEM observation confirmed that the surface of the obtained ethylene polymer particles had a large number of thread-like shapes mainly having a thickness of 0.3 μm to 0.5 μm and a length of 3 μm to 10 μm.

The ethylene polymer particles had an intrinsic viscosity and crystallinity almost similar to those of commercially available ultra high molecular weight polyethylene.
After the above-mentioned ethylene polymer particles were pressure-bonded at 130 ° C. to produce a sheet, stretching was attempted in an atmosphere of 125 ° C., but the sheet immediately broke.
Furthermore, the draw ratio was measured under the above conditions, and a result of 29 times was obtained.

  Since the ethylene polymer particles of the present invention have a high molecular weight and crystallinity and a specific surface shape, it is possible to obtain a molded product having high strength, particularly when solid phase stretch molding is performed. It can be used suitably for a use.

Claims (8)

(I) The intrinsic viscosity [η] is in the range of 5 dl / g to 30 dl / g,
(II) the degree of crystallinity is 80% or more,
(III) Ethylene polymer particles having a shape with a thickness of 0.1 μm to 3 μm and a length of 2 μm to 20 μm on the particle surface. The proportion of particles having a particle size of 355 μm or more is 2% by mass or less of the total,
The ethylene polymer particles according to claim 1, wherein the average particle size is 100 µm to 300 µm.   2. The ethylene polymer particles according to claim 1, obtained by reacting 500 g or more of ethylene per 1 g of the solid catalyst component. [A] a solid titanium catalyst component containing magnesium, halogen, titanium, and
[B] an organometallic compound catalyst component containing a metal element selected from Group 1, Group 2 and Group 13 of the Periodic Table;
The ethylene polymer particles according to claim 1, which are obtained by polymerizing an olefin containing ethylene in the presence of an olefin polymerization catalyst containing. [A] a solid titanium catalyst component containing magnesium, halogen, titanium, and
[B] an organometallic compound catalyst component containing a metal element selected from Group 1, Group 2 and Group 13 of the Periodic Table;
Including the step of polymerizing an olefin containing ethylene in the presence of an olefin polymerization catalyst containing, and maintaining the polymer obtained in the step at a temperature of 100 ° C. or higher and a melting point or lower for 15 minutes to 24 hours, A method for producing the ethylene polymer particles according to claim 1. (A) a step of producing an ethylene polymer having an intrinsic viscosity [η] of 2 dl / g or more and less than 10 dl / g;
(B) including a step of producing an ethylene polymer having an intrinsic viscosity [η] of 5 dl / g or more and 35 dl / g or less,
Per 100% by mass of the total ethylene polymer produced in the above process,
The proportion of the ethylene polymer produced in the step a is 0 to 50% by mass, the proportion of the ethylene polymer produced in the step b is 100 to 50% by mass,
The method for producing ethylene polymer particles according to claim 1, wherein the intrinsic viscosity [η] of the ethylene polymer produced in the step a is lower than the intrinsic viscosity [η] of the ethylene polymer produced in the step b. .   A molded product obtained by using the ethylene polymer particles according to claim 1.   The molded product according to claim 7 obtained by a solid phase stretch molding method.